DE2832490A1 - METHOD FOR REMOVING GASEOUS SULFURIZED BY-PRODUCTS - Google Patents

Description

Process for removing gaseous sulfur-containing by-products

The invention relates to a method for removing gaseous sulfur-containing by-products of streams, e.g. B. the chimney flue gases from high-temperature chemical processes.

Sulfur-containing gases are currently a significant one Many high temperature chemical processes produce exhaust gases that contain sulfur-containing materials as by-products included in the reaction. Such sulfur-containing gases are contained in the exhaust gases of many technical processes, especially those processes using coal, oil or other fossil fuels Use fuels as input materials. The removal of the sulfur content from the exhaust gas of such processes or the reduction to an acceptable level in terms of environmental pollution has been found to be practically economically unsustainable proven.

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On the other hand, there may be the presence of sulphurous gases very disadvantageous in the exhaust gases of many important technical processes be. When discharged directly into a chimney, they lead to air pollution that cannot be tolerated, if such gases are contained in the chimney in a concentration of more than a few tenths of a percent. Often it will Process waste gas used as feedstock for other processes in which the achievable yields require the application of a Require catalysis. However, gases containing sulfur are (even in small percentages) due to their tendency to poison the catalyst feared. In such processes, the removal of sulphurous gases prior to contact with the Catalyst essential.

To avoid problems with sulfur-containing exhaust gases, it is It is customary to use purified feedstock from which the sulfur content has been partially or practically completely removed or to use a chemical gas scrubber to remove sulphurous gases directly from the exhaust gas. Both methods, however, come with great cost and a significant disadvantage in using sulfur-containing ones Raw materials connected. Examples of some engineering processes where sulfur impurities in the process feed or are difficult or impossible to avoid in the chimney flue gas are listed in Table I.

When Hnight process gaseous sulfur-containing by-products from exhaust gases at a temperature of 93-816 ⁰ C (200 to 1500 ⁰ F) are removed by subjecting the gases to the action of crushed in the alkali metal and alkaline earth metal carbonates heat. The crushed in the heat materials are prepared by subjecting the carbonates of the exposure to high temperatures from 1093 to 2205 ⁰ C (4000 ⁰ F 2OCD up) and eiaen rapid "temperature rise

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Table I.

O CO OO CO

Reaction type catalyst atmosphere gaseous compounds

1) Water gas reaction with coal feed: C + H ₂ O - ♦ CO + H ₂

2) Fischer-Tropsch reaction: 2H ₂ + CO- * CH ₅ OH

3) Steam shift reaction: CO + H ₂ O -> H ₂ + CO ₂

4) methanation:

2H ₂ + 2CO - »CH ₄ + CO ₂

5) Burning coal to generate steam:

C O

p C +

CO

6) Roasting sulphide ores: Cu ₂ S + 2O ₂ - ♦ 2CuO + SO ₂ H ₂ S, COS, CS ₂

- ■ reducing the sulfur content

the coal

Raney-NicTcel reducing SO ₂ pollution im

used gas

platinum

reducing SO ₂ contamination in the

used gas

Raney nickel reducing SO ₂ contamination im

used gas

- oxidizing S0 _? from the sulfur content of the coal

oxidizing SO ₂ emission

• (ο ·

of the particles causes pressure to be created in the particles so that they break up or burst into much smaller particles. The process results in thermally comminuted particles having a particle size predominantly in the range from 0.1 to 100 µm and an average particle size from 1 to 20 µm. The exhaust gas temperature will not be above 816 ⁰ C (1500 ⁰ F) so that it does not come to corrosion (US-PS 4 018 868).

Further, a process for the removal of exhaust gases from SOp known (GrB-PS 396 969), in which preferably leads the exhaust gases by aqueous suspensions of ash from the coal combustion at 'temperatures of the aqueous suspension of 40 to 60 ⁰ G. However, it was not obvious to use ash in the Knight process, since one does not work in an environment with solids and hot gases.

The object of the invention is to provide an inexpensive method for removal of sulfur-containing constituents (by-products) from the exhaust gas from high-temperature chemical processes.

A further object of the invention is to provide a method for removing gaseous sulfur-containing by-products from high-temperature reaction products Provide chemical process, which is essentially characterized in that one

(1) a simple or complex metal oxide in the form of a coarse crushed powder in a transport gas through a high energy transfer zone leads, whereby the powder is subjected to temperatures that are sufficient to evaporate the powder, and the powder evaporates into a hot exhaust gas stream, the metalloid vapor contains,

(2) the hot exhaust gas stream with the content of metal oxide vapor

into the gaseous reaction product with a content of gaseous Sulfur-containing by-product of a high chemical temperature initiates the door procedure,

(3) allows the metal oxide vapor to condense into solid particles by reacting with the gaseous sulfur-containing by-product and thereby binds the sulfur content in the form of solid particles and

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(4) the solid particles containing essentially all of the sulfur content contained, separated from the gaseous reaction product.

The object of the present invention is as follows

Description in more detail. Show it:

Figure 1 is a flow diagram of a method according to the invention

and
FIG. 2 shows a graphic representation of the effect of ash evaporated in the arch on the SOg concentration

of an exhaust gas.

According to the invention, a method for desulfurizing the process exhaust gases from high-temperature chemical processes is now provided, that is both practical and effective and much cheaper than is a common gas scrubber. The essence of the invention consists in that the exhaust gas from a high-energy transmission zone, for example an electric arc, is introduced into the sulfur-containing gas stream a common carrier gas with entrained special pesticides feeds. These solids consist either of simple metal oxides or more complex derivatives, e.g. metal carbonates or silicates or mixed oxides (multiple oxides), the Represent combinations of two or more simple oxides.

In particular, the invention relates to a method for removing sulfur-containing by-products from high temperature reaction products chemical process, which is essentially characterized in that one

(1) A simple or complex metal oxide in the form of a coarsely comminuted powder in a conventional carrier gas through a high-energy transfer zone, the powder being subjected to temperatures which are sufficiently high to evaporate the powder, and the powder is essentially completely hot Exhaust gas with a content of metal oxide vapor evaporates _f

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(2) the hot exhaust gas with the content of metal oxide vapor in one Gaseous reaction product with a content of gaseous sulfur-containing by-product from a high-temperature chemical process initiates,

(3) the metal oxide vapor into ultra-fine, reactive particulate matter condense and with the gaseous sulphurous By-product can react, whereby one binds the sulfur content in the form of solid particles and

(4) the solid particles containing essentially all of the sulfur content contained, separated from the gaseous reaction product.

To carry out this process, it is only necessary to introduce a jet of a hot exhaust gas stream with a content of metal oxide vapor into the process reactor and / or the exhaust gas line from the process reactor, which is produced by absorbing a relatively coarse powder of a simple or complex metal oxide in a suitable working gas, such as air, CO and / or Hp, and was generated by introducing or passing the coarse powder taken into or through a high-energy heat transfer zone, e.g. an induction furnace, a solar furnace, a resistance furnace or an arc plasma generator, whereby the entrained coarse powder is decomposed into simple oxides in the case of a complex molecular composition and the simple oxides ^{are evaporated at temperatures generally above 2000 °} K with the formation of a hot exhaust gas jet. The oxide vapor is then condensed into an ultra-fine, highly reactive smoke inside the process reactor or in the discharge line, where the ambient temperature and other conditions favor a reaction between the oxide smoke and the sulfur gases, resulting in solid particles of metal sulfides, sulfites or sulfates forms, wherein the solid particles are then removed from the gas stream in the usual way, for example with bag filters, agglomerators and cyclones or electrostatic precipitators.

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As a result of the treatment of the sulfur-binding oxides up to very high temperatures of generally more than 2000 ^° K and preferably higher temperatures of, for example, more than 2500 ^° K, it is possible to use practically all metal oxides including mineral waste.

One of the most effective methods of achieving this hot exhaust gas stream containing metal oxide vapor is to use the methods and devices disclosed in US Patents 3,644,781 and 3,644,782. These US Patents describe an apparatus and method for excitation a fluid medium containing an entrained condensed phase, aB a powder of a simple or complex metal oxide, by an arc discharge between an anode and a cathode with a conical tip, the arc discharge having a contraction of the current-carrying area in the transition area in the vicinity of the cathode, the points of curvature of the contraction of the current-carrying area (when stretched) form an angle alpha, a fluid medium being forced along the conical tip of the cathode into and through the contraction of the current-carrying area in the transition area in the vicinity of the cathode at a mass flow density i leads to a substantially constant convection rate which is at least sufficient to cause an increase in the temperature of the arc column at a constant flow rate and below a total fluid medium convection rate at a substantially constant mass flow density which is sufficient to achieve the Lower angle alpha below 40 ° at a constant flow rate, and add a finely dispersed, non-gaseous medium which can cause an increase in the angle alpha of the fluid medium, which is forced along the conical tip at a total convection rate of the liquid medium at substantially constant total mass flow density, which is below the value required to reduce the enlarged angle alpha below 40 ° at a con-

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ORIGINAL INSPECTED

dammed flow rate is sufficient. This process is generally associated with the term forced convection cathode (FCC).

When performing the method according to the invention using of the devices and methods of US Pat. No. 3,644,781, it is essential that the entrained condensed phase of the powder a simple or complex metal oxide can penetrate the central core of the arc column as completely as possible, so that it is thereby vaporized and possibly broken down into two or more simple oxides before it leaves the arc discharge. It has been shown (US Pat. No. 3,644,781) that this treatment can evaporate most of a solid feedstock is effective when properly inserted into the conduction column of the arch.

When metal oxides are vaporized in this way, they very quickly condense into smoke on exiting the arc discharge. The ability to bind sulfur according to the invention depends on the specific physical and chemical properties of this smoke. For example, refractory materials, like most metal oxides, condense after evaporation in an electric arc to form ultrafine particles, usually in the range of 100 to 1000 S. Thus, a small amount of these solids has an enormous specific surface area, typically in the range of 50 to 300 m / g . Such a large specific surface enables effective adsorption of gaseous components from a gas stream in which the smoke is dispersed. Furthermore, when the sheet feed is made up of complex compounds, such as clay or slate, the process of evaporation results in the chemical breakdown of complex molecules. Furthermore, the extremely rapid vapor condensation of refractory materials in the arc exhaust favors a recombination in the form of chemically reactive simple oxides, which can be reproduced as follows for feldspar, for example:

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K ₂ O. Al ₂ O ₅ . 6SiO ₂ ■ * K ₂ O + Al ₃ O ₅ + 6SiO ₂ .

While the complex silicate molecule is quite stable and does not react with sulfur gases at the usual process ^{temperatures (eg 538 to 1649 0} C or 1000 to 3000 ⁰ P), simple oxides such as K ₃ O and Al ₂ O ₅ and a large number of others react Oxides, including the oxides of the alkali and alkaline earth metals, rapidly react with sulfur gases at these temperatures. Finally, the rapid condensation of the supercooled vapors emerging from the arc column causes the particles with highly active surfaces to solidify so that even usually non-reactive materials such as SiO ₂ are effective for surface adsorption and can promote the removal of sulfur gases from a process stream .

It should be emphasized that the properties mentioned, namely ultrafine particle size, high chemical reactivity and enlarged Surface adsorption capacity, characteristic only of evaporated materials and especially of materials which are vaporized in a high energy transfer zone such as an electric arc.

It is believed that the desulfurization effect produced in the exhaust gases from reactions with coal or petroleum feed was observed, basically on chemical reactions between metal oxides in the ultra-fine reactive state and the sulfur-containing gases in the exhaust gas. They are given by the following equations for a reducing or oxidizing Atmosphere explained:

(1) Reducing atmosphere (sulphurous gas - H ₂ S)

H ₂ S + MeO + MeSl + H ₂ O

(2) Oxidizing atmosphere (sulphurous gas - SO ₂ )

SO ₂ + MeO + ^ O ₂ -> MeSO ₄ I.

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where "Me" means any metal used in the preceding Examples is divalent.

In both examples, a sulfur-containing gas reacts with a Metal oxide with formation of a sulfur compound, which is a solid at the prevailing reaction temperatures. the Solid sulfur compounds are then removed from the gas stream by conventional means, such as a baghouse or electrostatic © ine Deposition.

The desulfurization processes currently being investigated include the use of fully or partially calcined lime or dolomite to react with HpS or SOp according to reactions (1) and (2), respectively, where Me = Ca for lime and = Ca or Mg for dolomite. These oxides are used, for example, in a finely crushed state in a fluidized bed burner (combustor) together with coal with a high sulfur content to generate energy. The temperatures in the combustion chamber of the steam generator are usually in the range from 1093 to 1260 ^° C. (2000 to 2300 ^° P). Under these conditions with calcined lime and excess air, reaction (2) takes place; the S0 ₂ amount, which is bound as CaSO, sufficient to Restraenge the SOG in the chimney to acceptable levels depress (less than 1000 ppm). However, the kinetics of this reaction in the working temperature range is such that, in the case of a satisfactory desulphurization, large amounts of lime per tonne of burnt coal must be processed; In addition, there is a very large system and high capital expenditure.

It should also be pointed out that the finely divided oxide particles used have sizes which are 10 ² ~ to 10 ⁵ times larger than that of the smoke condensate of the evaporated material according to the invention.

On the other hand, lime that has evaporated in the arch can enter the combustion chamber of a common burner for powdered cabbage

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will react effectively with SOp at the same temperature at a considerably greater rate due to the extremely small particle size and the high degree of reactivity of the material being vaporized in the arc, so that an actual quantitative conversion of SO ₂ to CaSO. occurs during the usual residence time of the gases in the combustion chamber. Accordingly, the amount of lime used for desulfurization is reduced, and (most importantly) the size and cost of the desulfurization aid device are substantially reduced.

The simple or complex metal oxide used in the process according to the invention can be any oxide as stated above. When desulfurizing the combustion gases when burning coal with a high sulfur content a waste mineral in the form of coal ash can be used for this purpose. Coal ash generally consists of clay and Slates, which are inert as sulfur adsorbents. In the high temperature zone, however, the stable complex silicates become broken down into reactive simple oxides, which are thereby effective in removing sulfur gases. This can create a waste material can be used in place of the scrubber feed, thereby significantly reducing process costs. Also be does not exacerbate the waste disposal problems, which is the case when large quantities of lime or dolomite are supplied or have to be removed.

The differences between the Knight method and the inventive method The procedures are as follows:

(1) The vaporization of a particular adsorbent (usually metal oxides) requires temperatures well above 2477.5 ⁰ C (4000 ⁰ F), whereas the known heat crushing method is limited to the range from 1093 to 2204 ⁰ C (2000 to 4000 ⁰ F) .

(2) The heat crushing treatment depends on the formation of gaseous decomposition products in the coarse particles, which

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burst as a result of the internal pressure. As a result, the starting materials are restricted to hydrates and carbonates of alkali metal and alkaline earth metal compounds which supply water vapor and / or gaseous carbon dioxide through thermal dehydration and / or COg evolution. In contrast, according to the invention, any material can be comminuted regardless of its composition; even materials that do not contain any gaseous decomposition products can be comminuted, for example CaO, Al ₂ O, coal ash or blast furnace slag.

(3) -The mean particle size of the heat-shredded material in the Knight process is in the range from 1 to 20 p, while the mean particle size of the smoke in the high energy transfer zone ranges from 0.01 to 0.1 jurassic (100 to 1000 S). Since the specific surface area for adsorbing e.g. SOp is inversely proportional to the square of the mean diameter, smoke according to the invention is 10,000 ° times Surface area per unit weight of material compared to thermally crushed material.

(4) While the surface properties of the thermally comminuted material in terms of chemical reactivity are essentially the same as those of the coarse feedstock, the surface of the smoke according to the invention shows a substantially increased reactivity towards said feedstock. This is believed to be due to the extremely rapid rate of condensation of the vapor from the high energy transfer zone according to the invention, which prevents orientation of the surface atoms to a naturally stable configuration. This means that the high surface energy of the particles is "frozen" as a result of the rapid rate of solidification. This results from processes such as sintering, which takes place at unusually low temperatures, or from chemical reactions which are considerably accelerated by high surface energies .

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From the foregoing it follows that the evaporation in the high-energy transfer zone is not just an alternative method of comminution, but a completely different method which yields a fundamentally different product. Furthermore, the new and unusual properties of the smoke from the high energy transfer zone form the basis for substantial improvements in the desulfurization process over thermally comminuted materials, the outcome of which could not be predicted. After the Knight method, the thermally crushed material is injected into the exhaust line at a location where the gas preferably has a temperature in the range of 93 to ⁰ 816 G (200 to 1500 ⁰ F) possesses. At the lower end of this range, the rate of adsorption for SOp becomes so slow that the process becomes ineffective. For a useful adsorption the Knight method, close to the upper limit value of 816 ⁰ C must (1500 ⁰ F) are performed. This makes implementation problematic. These include the fact that the use of Nahcolite (nahcolite) forms sodium hydroxide in the exhaust gas due to the presence of significant amounts of water vapor in the exhaust gas. It is a highly corrosive material; while it is at 816 ⁰ C (1500 ⁰ F) less corrosive than at 1093 ⁰ C (2000 ⁰ F), it is even more corrosive below 138 ⁰ C (1000 ⁰ F). So-Knight process is at least acknowledged that temperatures of the exhaust gas above 816 ⁰ G (1500 ⁰ F) are problematic for. Second, unless expensive heat transfer equipment is placed downstream, a significant amount of heat is wasted in high temperature desulfurization.

In contrast, the high specific surface area and the high reactivity of the smoke of the high-energy transfer zone enable efficient adsorption of SO ₂ at relatively low temperatures. For example, it has been found that thermally crushed lime (calcined lime) is _{completely ineffective for adsorbing SO 2} at 177 ^° C. (350 ^° F.), while CaO evaporated in an FCC arc

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effectively adsorbed at this temperature. It is interesting to note that this is the temperature in which exhaust gases are discharged from the chimney of conventional power plants. Accordingly, the energy balance is maximal; one Corrosion due to addition of an SOp adsorbent becomes by using FCC arc smoke at low temperatures excluded, which is not possible with the Knight process.

It could also be demonstrated that fly ash from coal, which in its original state is as finely divided as it is thermally Crushed Nahcolit is completely ineffective when used in its original state to desulfurize a sulfur-containing exhaust gas is. After being treated in an FCC arc, the ashes become however, an effective adsorbent.

In the known wet washing process, exhaust gas is passed through water, which dissolves, for example, SO ₉ , NO and HCl from the exhaust gas of metallurgical plants. As a result of the presence of oxidizing compounds, for example oxides of iron and manganese, the acidic gases are converted to, for example, H ₂ SO., HNO, and HGl in the aqueous solution. You can then dissolve metal oxides in the exhaust dust. The fact that these are ash constituents has no connection with the finding according to the invention that evaporated fly ash, in contrast to non-evaporated fly ash, can desulfurize exhaust gas. In any case, the known wet washing process bears no resemblance to the adsorption of gaseous contaminants on the surface of injected aerosols. The invention is explained in more detail below by means of an example.

Example desulfurization process

The device corresponded to FIG. 1. In the case of the fluid convection cathode 1 was a double-jacket cathode according to FIG

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.17-

US Pat. No. 3,900,762. It was supplied through line 2 with an oxide powder in a carrier gas. The carrier gas was passed from the line 3 through the mixing valve 4, where the oxide powder from the funnel 5 was mixed with the carrier gas. The positive pole was formed by three anodes 6, which were fluid flow anodes according to US Pat. No. 3,209,193, which were arranged symmetrically at a distance from the cathode axis according to US Pat. No. 3,931,542. The hot exhaust gas containing metal oxide vapors was collected in the hood 7 and passed through a mixing zone 8 together with SOp, which was introduced at 9 after draining from the S0 ₂ tank 10 via the line 11, the valve 12 and the flow meter 13 became. At the upper end of the mixing zone 8, the temperature was measured with a thermocouple 14. The exhaust gas was then passed through a reaction zone 15, where at 16 a sample of the exhaust gas was collected in line 17 and passed through a solids filter 18; the SOg content was measured in detector 19. A positive flow was maintained by the action of the fan 20; the gases were then released into the chimney 21.

The oxide powder used was plug ash from a commercial coalburning power generating station). This consists essentially of complex silicates, such as slate and clay, which make up a large one Percentage of suitable metal oxides included. The ashes became into the funnel of a vibrating Fulverzufuhreinriehbunp; Λ release and fed via the control valve 4 to the high energy transmission zone, which in this case is through the column of an electric arc was formed. The arch system preferred for this purpose was a double barbed fluid convection cathode (FCC) 1 according to US Pat. No. 3,900,762. The positive pole was replaced by three Fluid flow anodes (FTA) 6 (according to US Pat. No. 3,209,193) are formed, which were arranged symmetrically about the extension of the cathode axis according to US Pat. No. 3,931,542.

The arc exhaust gas was together with tempering air from the

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ambient atmosphere is sucked into the mixing zone 8 and the reaction zone via the hood 7 directly above the arch with the aid of the fan 20 downstream of the reaction zone. The mixing zone 8 consisted of a stainless steel pipe (1.2 m χ 5 cm = 4 I ¹ US χ 2 "; ID). The gaseous sulfur dioxide was fed into the mixing zone 8 immediately after the hood 7 at 9, the flow through the Valve 12 was controlled and measured by flow meter 13. Operation of fan 20 was adjusted to draw in about 1.1 nr (4-0 cubic feet) / min of gas which was a mixture of arc exhaust and tempering air with SOp , which was initiated at 9. The volume otrömungorate through the mixing zone was adjusted so that an exit temperature of about 1204 ⁰ C (2200 ⁰ P) was reached, which was determined with a thermocouple 14 at the end of the mixing zone 8. The flow of the SOp in the tube at 9 was adjusted with respect to the amount of gas drawn into the hood so that the gas collected at 16 near the downstream end of the reactor zone 15 was 1800 parts per million on the SOg meter 19 indicated.

After the SOp current was set, the arc was ignited and adjusted so that 70 g / min argon in the inner jacket and about 0.057 m (2 cubic feet; standard) / min in the outer jacket the double jacket Fluidumkonvektionska method 1 were passed. At the same time, 15 g / min argon was fed to each of the three porous FTA anodes 6. The arc spacing was set to 6.3 cm (2-1 / 2 in inch) set; Current and voltage were 600 A (in total) and 130 V. After that, the argon in the outer jacket was min of air (2.5 SCPM), after which the arc voltage is increased to 160 7 rise.

As soon as the argon in the outer jacket had been replaced by air, the reading on the SO ₂ measuring device rose to about 2000 parts per million and then fell to about 1700 ppm in 1 to 2 minutes, where it remained. The arc was operated under these conditions for 3 to 4 minutes, the temperature of the gas stream at

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14 rose to the constant value of 1204 ⁰ C (2200 ⁰ P). The SO ₂ measuring device 19 constantly showed 1700 ppm. The ash funnel was then opened and set to a feed of 38 g ash / min. It was carried away by the airflow into the FCC outer jacket. An incandescent flue gas flame of vaporized ash components was immediately visible at the entrance to the hood above the arch. After about 1/2 minute the S0 ₂ measuring device 19 fell off. The readings (beginning with the time the ash is fed to the arch) are shown graphically in FIG. Within 3 minutes, the SOg concentration in the gas collected at 16 dropped to less than 200 ppm. This low value remained constant until the ash feed was stopped and the arc turned off, after which the SOg reading rose again to the value of 1800 ppm.

It follows conclusively that the ash evaporated in the arc can remove practically all of the SOp from a gas stream with 1700 ppm SOp.

The invention thus relates to a method for removing sulfur-containing by-products from the high-temperature reaction products chemical process, which essentially consists in that one

(1) A simple or complex metal oxide in the form of a coarsely comminuted powder in a conveying gas passes through a high-energy transmission zone, thereby heating the powder in such a way that the powder can be vaporized, and the powder is vaporized essentially with the formation of a hot exhaust gas of metal oxide vapor,

(2) the hot exhaust gas from metal oxide vapor into a gaseous one Reaction product with a content of sulfur-containing by-products a chemical high-temperature process,

(3) the metal oxide vapor into solid particles to react with lets the sulfur-containing by-product condense and the Sulfur content in the form of solid particles binds. And

(4) separating the solid particles, which contain substantially all of the sulfur content of the sulfur -containing by-product, from the gaseous reaction product.

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Claims (7)

Claims 1. Process for removing gaseous sulfur-containing by-products from high-temperature reactive products chemical process, characterized in that one (1) a simple or complex metal oxide in the form of a coarsely crushed powder in a common carrier gas through a High energy transfer zone leads, which makes the powder sufficient subjected to high temperatures to vaporize the powder, and the powder essentially forming a evaporates hot exhaust gas containing metal oxide vapor, (2) the hot exhaust gas containing metal oxide vapor into a gaseous reaction product containing gaseous injecting sulfur-containing by-products from a high-temperature chemical process, (3) Let the metal oxide vapor condense into ultrafine, reactive solid particles, then the particles with the gaseous ones brings together sulfur-containing by-products and thereby binds the sulfur content in the form of solid particles and (4) separates the solid particles, which are essentially the total amount the sulfur content of the gaseous reaction product. 2. The method according to claim 1, characterized in that there is an electrical as the high-energy transmission zone Bow used. 3. The method according to claim 2, characterized in that a forced convection cathode is used as the electric arc used. 4. The method according to any one of the preceding claims, characterized in that the gaseous sulfur-containing By-product from the combustion of coal as a high-temperature chemical process is used. Sheer-PI60678-Bo-HÖ 809886 / 089S ORIGINAL INSPECTED 5. The method according to any one of the preceding claims, characterized in that the gaseous sulfur-containing By-product from roasting metal sulfide ores as a chemical Uses high temperature processes. 6. The method according to any one of the preceding claims, characterized in that it is the metal oxides It is constituents of ash from coal combustion. 7. The method according to any one of the preceding claims, characterized in that the metal oxides are components of slag from the melting of sulfide ores . Sheer-P1 60678-Bo-Hö 809886/0895